KR20130046344A - Dynamic gas distributor and a bubble column comprising the dynamic gas distributor - Google Patents

Abstract

PURPOSE: A dynamic gas distributor and a bubble column reactor applying the same are provided to improve a catalyst and a reaction efficiency in the reactor main body and to prevent a malfunction of the dynamic gas distributor and the loss of the catalyst by minimizing the back flow of the slurry in the reactor main body to the dynamic gas distributor during the reaction or at the completion of reaction. CONSTITUTION: A bubble column reactor comprises a reactor main body(10) and a dynamic gas distributor(20) arranged to be connected to the lower part of the reactor main body. The reactor main body stores the slurry containing the catalyst. The synthetic fuel is produced by the reaction of the slurry containing the catalyst with the synthesis gas introduced in the main body. The gas distributor disperses the synthesis gas supplied through the inlet tube(24) by rotation, converts the dispersed synthesis gas into the uniform bubble particle, and supplies this to the inside of the reactor main body.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a dynamic gas distributor and a bubble column reactor using the dynamic gas distributor,

The present invention relates to a bubble column reactor, and more particularly, to a bubble column reactor in which bubbles of an incoming syngas are uniformly converted, and a wake (flow of disturbed air) The present invention relates to a dynamic gas distributor and a bubble column reactor employing the dynamic gas distributor.

In general, bubble column reactors have advantages of high heat and mass transfer and are widely used in reactions such as biochemical reactions, wastewater treatment and coal liquefaction reactions.

In this bubble column reactor, the reaction takes place while the gaseous reactant (synthesis gas) passes through the continuous phase composed of the catalyst and the product.

At this time, the mass transfer rate through uniform contact and dispersion between the reactant (synthesis gas) and the catalyst is very important as a parameter for determining the reaction efficiency.

Here, as a main means for increasing the mass transfer rate of the reactive gas, a method of increasing the fluidity in the reactor and a method of increasing the gas capture rate in the continuous phase are mainly utilized.

Generally, the fluid flow in a bubble column reactor is divided into two main areas: a homogeneous flow region and a non-homogeneous flow region.

A homogeneous flow region occurs at a lower flow velocity of the gas, while a non-homogeneous flow region forms at a higher flow velocity.

Therefore, in a reaction requiring a high reaction yield, it is common to carry out the reaction in a non-uniform flow region having excellent flowability of the continuous phase.

Another method of increasing the mass transfer rate in the reactor is to increase the gas capture rate. The gas capture rate is defined as the volume fraction of gas present in the continuous phase.

According to Letzel et al. (1999), the ratio of gas capture rate to mass transfer rate of reactant gas is about 0.5, which is constant. Therefore, increasing the gas capture rate is an important parameter for increasing the mass transfer rate.

In general, the gas capture rate is affected by the linear velocity of the reaction gas, the reactor diameter, the physical properties of the continuous phase, and the like.

That is, as the linear velocity of the reaction gas increases, as the diameter of the reactor decreases, and as the viscosity and surface tension of the continuous phase decrease, the gas capture rate tends to increase in the reactor.

The research on the change of the gas capture rate according to the reaction condition or the reaction additive has been carried out much. However, the research on the gas capture rate according to the reactor design is limited.

In general, the rising velocity of bubbles is closely related to the size and size distribution of bubble particles.

That is, the rising velocity of the bubbles increases in proportion to the square of the size of the bubble particle.

In addition, when bubble particles of various sizes coexist, the frequency of collision between the bubbles increases because the difference in the rising velocity between the bubble particles increases. These high impact frequencies can lead to the formation of large bubble particles because they lead to cohesion between the bubble particles.

The increase in the bubble rising rate is negative in terms of gas capture rate, since it leads to a decrease in the residence time in the reactor during the unit time.

Thus, the technique of controlling the size of the bubble particles entering the reactor is very essential for enhancing the reactor efficiency.

So far, many researchers have applied various gas distributor types to control the size of these bubble particles.

As a representative example thereof, a porous gas distribution plate, a porous gas distribution pipe, a metal foam, and the like can be considered.

They were able to optimize the design of the gas distributor by systematically analyzing the effect of pore size and pore gap on the size distribution of gas bubbles.

However, these studies have not been able to overcome the limitations caused by the use of a gas dispersion plate fixed in a certain shape.

That is, it is impossible to control it because the bubble is formed through the constantly opened pores.

It is presumed that the bubble column formed at this time appears as the wake formed at the rear end of the bubble particle rising earlier promotes the rising velocity of the following bubble particle.

Accordingly, there is a need for a device capable of eliminating bubble columns due to wakes and controlling the size of bubble particles in a desired shape.

SUMMARY OF THE INVENTION It is a first object of the present invention to provide an apparatus and a method for uniformly changing bubble particles of a syngas to be subjected to a Fischer-Tropsch reaction with a catalyst in a reactor body, A dynamic gas distributor capable of increasing the reaction efficiency with the catalyst in the reactor main body by suppressing a phenomenon in which bubbles are generated by a wake (flow of disturbed air) generated at the rear end of the bubble particle, and a bubble column reactor employing the dynamic gas distributor .

The second object of the present invention is to prevent the slurry inside the reactor body from flowing back to the dynamic gas distributor when the reactor body is operated or stopped, The present invention also provides a dynamic gas distributor and a bubble column reactor employing the dynamic gas distributor which can prevent the reverse flow of the slurry by stopping the rotary disk at a predetermined position and eliminating or minimizing the opening of the fixed dispersion disk when the reactor is terminated have.

In order to achieve the above object, the present invention provides a bubble column reactor including a reactor body and a dynamic gas distributor. The reactor body stores a slurry containing the catalyst, and the slurry containing the catalyst reacts with the incoming synthesis gas to produce a synthetic fuel. The dynamic gas distributor is disposed in communication with the lower portion of the reactor main body. The dynamic gas distributor disperses the syngas supplied through the inlet pipe by rotation, converts the dispersed syngas into uniform bubble particles, do.

In the bubble column reactor according to the present invention, the dynamic gas distributor includes a stationary dispersion disk, a mixing container, and a gas dispersion means. The fixed dispersion disk has a plurality of openings formed on the surface thereof to convert the bubble particles of the syngas supplied through the inlet pipe to a uniform size. The mixing tube extends vertically downward to the rim of the stationary dispersion disk, guides the synthesis gas supplied through the inlet pipe, and mixes the mixture at a constant composition and pressure. The gas distributing means distributes the syngas introduced into the blending container by rotation and provides the dispersion gas to the fixed dispersion disk.

In the bubble column reactor according to the present invention, the gas dispersion means includes a rotary disk and a drive means. The rotating disk is spaced apart from the lower portion of the fixed dispersion disk to control the opening / closing cycle of the aperture. The driving means is disposed outside the compounding cylinder to rotate the rotary disk.

In the bubble column reactor according to the present invention, the rotary disk includes a semicircular disk, a plurality of arc-shaped disks formed symmetrically, a semicircular disk having a plurality of openings, a plurality of arc-shaped disks formed with a plurality of openings, And a circular disk having an open aperture of a circular disk.

In the bubble column reactor according to the present invention, the opening of the rotary disk may be in the range of 10 to 90% of the circular disk.

In the bubble column reactor according to the present invention, the material of the rotary disk is selected from iron, copper, nickel, nickel-chromium alloy and iron-chromium-aluminum alloy which are hydrophobic materials having a contact angle to water of 80 ° or more. It can be one.

In the bubble column reactor according to the present invention, the driving means may be a magnetic mixer capable of operating at 50 atm or less.

In the bubble column reactor according to the present invention, the interval between the stationary dispersion disk and the rotary disk spaced apart from the lower disk may be in the range of 0.01 mm to 10 mm.

In the bubble column reactor according to the present invention, the rotational speed of the rotating disk may be proportional to the linear velocity of the syngas gas.

In the bubble column reactor according to the present invention, at least one rotary disk may be installed in the compounding cylinder.

In the bubble column reactor according to the present invention, at least one inlet pipe may be connected to a side surface of the compound container below the portion where the rotary disk is installed.

In the bubble column reactor according to the present invention, the size of the aperture diameter of the fixed dispersion disk may be in the range of 0.1 to 2 mm, and the aperture ratio may be in the range of 0.05 to 2.0%.

In the bubble column reactor according to the present invention, the catalyst contained in the slurry in the reactor main body may be iron, cobalt, copper, potassium, cesium, sodium, molybdenum, tungsten, zinc, nickel, rubidium, Rhodium and palladium, or a mixture of two or more thereof.

The bubble column reactor according to the present invention further comprises filtering means disposed on the upper side of the reactor body for filtering the catalyst and flowing out only the synthetic fuel produced by the reaction to the outside of the reactor body. An outflow pipe for discharging an unreacted synthesis gas and a chemical gas generated during the reaction to the outside of the reactor main body may be connected to the upper end of the reactor main body.

Further, the present invention is also a dynamic gas distributor provided in communication with the reactor body of the bubble column reactor, including a mixing container, a gas dispersion means and a fixed dispersion disk. The mixing tube has an opening formed at an upper portion thereof to be connected to the reactor body. The synthesis gas introduced through the inlet tube is temporarily stored and mixed at a constant composition and pressure. The gas distributing means disperses the syngas introduced into the blending container by rotation. The fixed dispersion disk is coupled to the opening of the compounding vessel and has a plurality of openings formed in its surface to convert the bubble particles of the synthesized gas dispersed by the gas dispersion means into a uniform size.

According to the bubble column reactor to which the dynamic gas distributor of the present invention is applied, it is possible to uniformly convert the bubble particles of the syngas to be reacted with the catalyst in the reactor main body and the Fischer-Tropsch, (wake: flow of perturbed air), it is possible to improve the reaction efficiency with the catalyst in the reactor main body.

It is also effective in minimizing the backflow of the slurry inside the reactor body to the dynamic gas distributor during or at the end of the reaction to prevent malfunction of the dynamic gas distributor and loss of catalyst

1 is a schematic view of a bubble column reactor to which a dynamic gas distributor according to the present invention is applied;
FIG. 2 is a perspective view of the dynamic gas distributor extracted in FIG. 1;
Figures 3 and 4 illustrate various embodiments of a rotating disc according to the present invention,
Fig. 5 also shows that in the various embodiments of the inflow pipe connected to the compounding cylinder according to the invention,
6 shows another embodiment of the gas distributing means according to the present invention,
7 is a photograph showing bubble particles discharged from a fixed dispersion disk of a bubble column reactor according to a comparative example,
8 is a conceptual diagram showing bubble particles in a bubble column reactor to which a dynamic gas distributor according to the present invention is applied,
FIG. 9 is a photograph showing the bubble particles discharged from the stationary dispersion disk of the bubble column reactor in FIG.

Hereinafter, a bubble column reactor using a dynamic gas distributor according to the present invention will be described in detail with reference to the accompanying drawings.

FIG. 2 is a perspective view of a dynamic gas distributor taken in FIG. 1, FIG. 3 is a view showing various embodiments of a rotating disk according to the present invention, FIG. Fig. 5 shows various embodiments of the inlet pipe connected to the compounding cylinder according to the present invention, and Fig. 6 shows another embodiment of the gas distributing means according to the present invention.

1 to 6, the present invention can be applied to the reactor main body 10 by more uniformly controlling the bubble particles of the syngas which reacts with the catalyst in the reactor main body 10 and the Fischer-Tropsch reaction, To a bubble column reactor (100) to which a dynamic gas distributor (20) having a structure capable of promoting mass transfer and reaction efficiency between a catalyst and a synthesis gas is applied.

The bubble column reactor 100 to which the dynamic gas distributor 20 is applied is combined with a wake (disturbed air flow) generated at the rear end of the uniformly converted bubble particles through the dynamic gas distributor 20, And a rotating gas distributing means (23) for preventing the phenomenon that the gas is dispersed.

The bubble column reactor 100 to which the dynamic gas distributor 20 of the present invention is applied is largely composed of three parts comprising a reactor body 10 having a filtering means 30 and an outlet tube 11, 10 and a dynamic gas distributor 20 for converting the syngas introduced through the inlet pipe 24 into uniform particles.

The reactor main body 10 is a structure in which a slurry (oil, wax) containing a catalyst that undergoes Fischer-Tropsch reaction with syngas is stored.

The catalyst contained in the slurry stored in the reactor body 10 is active for the Fischer-Tropsch reaction and the water gas shift reaction. Depending on the composition of the synthetic fuel obtained, iron, cobalt, copper, potassium , Cesium, sodium, molybdenum, tungsten, zinc, nickel, rubidium, rhodium, palladium, and the like.

In addition, the catalyst has a particle size distribution of 0.1 to 200 [mu] m to be uniformly injected into the reactor body 10. [ This is because if the particle size is smaller than 0.1 mu m, the catalyst will not be filtered by the filtering means 30, resulting in leakage of the catalyst. When the particle size is larger than 200 mu m, It is not preferable because uniform dispersion of the particles is difficult.

Here, the filtering means 30 discharges the synthetic fuel produced by the Fischer-Tropsch reaction and functions to filter the catalyst.

The filtering means 30 is disposed on the upper side of the reactor body 10 so that the catalyst functions to filter out only the synthetic fuel produced by the reaction.

The filtering means 30 may be constructed of a general stainless material and may have a pore size ranging from 0.1 um to 10 um, and most preferably a pore size of 1 um. When the filtering means 30 having a pore size of 1 um is used, the catalyst particles in the reactor body 10 can be filtered and selectively collected only the synthetic fuel.

The outflow pipe 11 functions to discharge the unreacted synthesis gas and the chemical gas (methane, propane, pentane, etc.) generated by the reaction in the reactor main body 10. Here, the chemical gas and the synthetic fuel are similar in that they are products by the Fischer-Tropsch reaction, but the chemical gas has a gas phase in the reaction condition and the synthetic fuel takes a liquid phase There is a difference.

The dynamic gas distributor 20 is connected to the lower portion of the reactor body 10 so as to convert bubble particles of the syngas supplied through the inlet pipe 24 into uniform bubble particles and supply the same to the inside of the reactor body 10. .

The dynamic gas distributor 20 includes a stationary dispersion disk 21, a mixing box 22, and a gas distributing means 23. The compounding tank 22 extends vertically downward at the rim of the stationary dispersion disk 21, and the inlet pipe 24 is connected. The gas distributing means 23 includes a rotating disk 231 housed inside the blending hopper 22 and a driving means 232 disposed outside the blending hopper 22 to rotate the rotating disk 231 .

Here, the fixed dispersion disk 21 has a plurality of apertures H formed on its surface, and functions to convert the bubble particles of the syngas supplied through the inflow pipe 24 into a uniform size. In this case, the diameter of the aperture H of the stationary dispersion disk 21 is preferably in the range of 0.1 mm to 2 mm, and the aperture diameter of the fixed dispersion disk 21 is preferably in the range of 0.05 to 2.0%.

When the total opening ratio of the opening hole H is smaller than 0.05%, the pressure drop of the syngas acting on the fixed dispersion disk 21 becomes very large. Therefore, the catalyst contained in the slurry in the reactor body 10 and the reaction The clogging phenomenon may occur due to the backflow of the synthetic fuel produced by the catalyst layer, and cracking of the catalyst particles injected into the continuous phase may be caused.

Further, if the opening ratio of the opening hole H is 2.0% or more, uniform injection of the syngas into the reactor main body 10 becomes difficult, so that the opening ratio is preferably limited within the range of 0.05 to 2.0%.

By limiting the opening ratio of the stationary dispersion disk 21 in the range of 0.05 to 2.0%, the syngas having a uniform particle distribution can provide sufficient fluidity to the continuous phase of the reactor body 10 to increase the contact with the catalyst and slurry Not only the production yield of the synthesis gas can be increased but also the reaction heat generated by the Fischer-Tropsch exothermic reaction can be released evenly to the outside.

The compounding box 22 is integrally coupled to the fixed dispersion disk 21, and more specifically, it has a structure in which it extends vertically downward to the rim of the fixed dispersion disk 21 and is coupled thereto. That is, the compounding tank 22 is formed with an opening 221 at a portion connected to the reactor main body 10, and the fixed dispersion disk 21 is coupled to the compounding tank 22 so as to cover the opening 211 do.

The compounding tank 22 temporarily stores the synthesis gas introduced through the inlet pipe 24 and mixes the synthesized gas at a constant composition and pressure. The inlet pipe 24 is provided with a flow rate controller 40 capable of controlling the flow rate of the syngas and a flow meter 50 for checking the flow rate of the gas in real time to select the synthetic fuel Can be improved.

Here, an example in which the inflow pipe 24 is provided so as to face the center of the compounding cylinder 22 as shown in Fig. 2 has been described, but the present invention is not limited thereto. For example, as shown in Fig. 5, a plurality of inflow pipes 24 may be installed in the compounding tank 22. As shown in Fig.

5A, a plurality of inflow pipes 24 are exposed to the inside of the compounding bottle 22 through the side surface of the compounding bottle 22 in the direction oblique to the center of the compounding bottle 22 at a predetermined angle, . 5B, a plurality of inflow pipes 24 may be inserted and protruded into the compounding tube 22, and the end of the inflow pipe 24 may be bent to one side. As shown in Fig. 5, by connecting the inlet pipe 24 to the compounding cylinder 22, it is possible to distribute the synthesis gas introduced into the compounding cylinder 22 more uniformly.

The gas distributing means 23 is disposed at a lower portion of the stationary dispersion disk 21 so that a wake generated at the rear end of the bubble particles converted into uniform particles through the opening H of the stationary dispersion disk 21, The flow of disturbed air) to prevent the phenomenon of bubble generation.

More specifically, the gas distributing means 23 includes a rotating disk 231 which is disposed at a lower portion of the stationary dispersion disk 21 and adjusts an opening / closing cycle of the opening hole H, And driving means 232 for rotating the rotating disk 231.

As shown in FIGS. 3 and 4A, 4B, 4C, 4D, 4E, 4F, and 4G, the rotating disk 231 includes a semicircular disk, a plurality of arc- A semi-circular disk having a plurality of openings, a plurality of arc-shaped disks formed with a plurality of openings and formed symmetrically with each other, and a circular disk having a plurality of openings formed therein.

At this time, it is preferable that the opening of the rotary disk 231 is in the range of 10 to 90% of the total size of the rotary disk 231. If the shape of the rotary disk 231 is irregular or the aperture ratio is less than 10% Unstable fluctuation occurs in the pressure inside the cylinder 22 and drift occurs in the flow of the synthesis gas flowing into the reactor main body 10. The occurrence of such drift is caused by the gas capture rate The reaction efficiency is lowered, which is not preferable.

Also, when the opening ratio of the rotary disk 231 is larger than 90%, the effect of suppressing the generation of the bubble column by the rotary disk 231 becomes very insignificant.

3 (d), in the case of a circular disk in which a plurality of apertures H are formed in the rotary disk 231, it is preferable to eliminate the opening of the fixed dispersion disk 21 at the end of the reactor 100 Or minimizing the backflow of the slurry.

In addition, the number of revolutions of the rotary disk 231 is proportional to the linear velocity of the syngas. Therefore, if the linear velocity of the incoming syngas is high, the wake becomes large to increase the number of revolutions of the rotary disk, and if the linear velocity of the syngas is low, the wake becomes small and the number of revolutions of the rotary disk 231 decreases.

The material of the rotating disk 231 is preferably selected from among iron, copper, nickel, nickel-chromium alloy, and iron-chrome-aluminum alloy, which are hydrophobic materials having a contact angle to water of 80 ° or more.

This is because if a hydrophilic material having a contact angle with water of less than 80 ° is used, the flow of the gas is not controlled by the opening / closing cycle of the pores, but is strongly influenced by the surface tension between the rotating disk 231 and the bubbles to be.

It is preferable that the rotating speed of the rotating disk 231 is 10,000 rpm or less. If the rotational speed is 10,000 rpm or more, the unit time in which small bubbles can permeate through the opening hole H is smaller than the unit time of opening and closing the pores The synthesis gas can not pass through the opening hole H of the stationary dispersion disk 21 and consequently the pressure inside the compound container 22 rises.

The rotating disk 231 is rotated at 10,000 rpm If you adjust the rotation speed to It is possible to minimize the generation of the bubble column due to the wake effect and to control the size of the generated bubble particle.

The driving unit 232 may be an electric motor, and more particularly, a magnetic mixer for rotating the rotating disk 231 at a constant speed. Such a magnetic mixer operates at a pressure of 50 atm or less and is capable of controlling the rotation speed to a constant level.

In particular, since the Fischer-Tropsch reaction in the reactor body 10 is generally operated at a pressure of 15 atm or higher, the rotary disk 231 can be stably rotated by using such a magnetic mixer.

On the other hand, the rotating disk 231 covers the opening hole H of the stationary dispersion disk 21 so that when the reactor main body 10 is operated or stopped, the slurry in the reactor main body 10 is returned to the dynamic gas distributor 20 The rotating disk 231 can be stopped and fixed at a predetermined position when the reactor 100 is terminated. In addition, the rotation of the rotating disk 231 can be kept constant to prevent the slurry from sinking, It is possible to prevent the reverse flow of the slurry by eliminating or minimizing the opening of the dispersion disk 21. [

The rotary disk 231 is installed close to the stationary dispersion disk 21 so as to stably control the opening / closing cycle of the aperture H of the stationary dispersion disk 21. [ For example, the gap between the stationary dispersion disk 21 and the rotary disk 231 spaced apart from the lower portion is preferably in the range of 0.01 mm to 10 mm.

If the distance between the fixed dispersion disk 21 and the rotary disk 231 is 0.01 mm or less, it is not preferable because the gas of the introduced synthesis gas is prevented from passing through the fixed dispersion disk 21, It is not preferable because a wake occurs again on a spaced gap.

In order to minimize the physical influence of the syngas flowing into the mixing cylinder 22 through the inlet pipe 24 directly to the rotating disk 231, The inlet tube 24 is connected to the portion of the compounding tube 22 below the position.

Here, as shown in Fig. 2, the rotary disk 231 has an example in which one is provided in the compounding cylinder 22, but the present invention is not limited thereto. For example, as shown in Fig. 6, a plurality of rotating discs 231a and 231b may be installed in the compounding cylinder 22. [ The plurality of rotating disks 231a and 231b may be installed above the inflow pipe 24.

A bubble column reactor 100 having a dynamic gas distributor 20 according to the present invention and a bubble column reactor according to a comparative example in which only a fixed dispersion disk is installed in a mixing column will be described below.

7 is a photograph showing the bubble particles discharged from the stationary dispersion disk 121 of the bubble column reactor according to the comparative example. FIG. 8 is a conceptual view showing bubble particles in a bubble column reactor to which a dynamic gas distributor 20 is applied, and FIG. 9 is a photograph showing bubble particles discharged from a fixed dispersion disk 21 of a bubble column reactor in FIG.

First, referring to FIG. 7, it can be confirmed that the size of the bubbles formed is not uniform because no separate gas distributing means is provided in this comparative example.

Further, in the bubble column reactor according to the comparative example, the introduced synthesis gas is not converted into uniform bubble particles through the opening hole of the stationary dispersion disk 121 but merged with a wake (flow of disturbed air) It is possible to confirm that it is generated.

However, as shown in FIGS. 8 and 9, in the bubble column reactor main body 10 to which the dynamic gas distributor 20 of the present invention is applied, the generation of wake is suppressed through the rotating disk 231 rotating inside the compounding cylinder 22 As a result, it can be confirmed that the bubble particles discharged into the opening hole H of the fixed dispersion disk 21 are uniformly changed.

As a result, the reaction efficiency with the catalyst in the reactor body 10 can be improved through the syngas having the uniform bubble particles, so that the yield of the synthesis fuel can be increased and the productivity can be increased.

Although the present invention has been described in connection with the preferred embodiments mentioned above, various other modifications and variations will be possible without departing from the spirit and scope of the invention. It is, therefore, to be understood that the appended claims are intended to cover such modifications and changes as fall within the true scope of the invention.

10: reactor body
11: Outflow tube
20: Dynamic gas distributor
21: Fixed distributed disk
22:
23: gas distribution means
231: Rotating Disk
232: driving means
24: inlet pipe
30: filtering means
40:
50: Flowmeter
H: opening ball
100: Bubble column reactor with dynamic gas distributor

Claims (20)

A slurry containing a catalyst is stored, and a slurry containing the catalyst is reacted with an incoming synthesis gas to produce a synthetic fuel;
A dynamic gas distributor disposed in communication with the lower part of the reaction base, distributing the syngas supplied through the inlet pipe in rotation, and converting the dispersed syngas into uniform bubble particles to supply the inside of the reaction base;
Bubble column reactor to which a dynamic gas distributor comprising a. 2. The apparatus according to claim 1, wherein the dynamic gas distributor
A fixed dispersion disk which has a plurality of openings formed in the surface thereof to convert the bubble particles of the syngas supplied through the inlet pipe to a uniform size;
A compounding cylinder extending vertically downward to a rim of the stationary dispersion disk and guiding the synthesis gas supplied through the inlet pipe to mix at a constant composition and pressure;
A gas dispersion means for dispersing the syngas introduced into the blending container by rotation and providing the dispersion gas to the fixed dispersion disk;
Wherein the bubble column reactor is a bubble column reactor. The gas dispersing means of claim 2,
A rotating disk spaced apart from a lower portion of the stationary dispersion disk to adjust an opening / closing cycle of the aperture;
Driving means disposed outside the compounding cylinder for rotating the rotary disk;
Wherein the bubble column reactor is a bubble column reactor. The method of claim 3,
The rotating disk may be any one selected from a semicircular disk, a plurality of arc-shaped disks formed symmetrically, a semicircular disk having a plurality of openings, a plurality of arc-shaped disks formed with a plurality of openings, and a circular disk having a plurality of openings formed therein And the bubble column reactor is a single bubble column reactor. The method of claim 3,
The opening ratio of the rotating disk is a bubble column reactor using a dynamic gas distributor, characterized in that 10 to 90% range compared to the circular disk. The method of claim 3,
The material of the rotating disk is any one selected from hydrophobic materials iron, copper, nickel, nickel-chromium alloy and iron-chromium-aluminum alloy having a contact angle to water of 80 ° or more. Bubble column reactor applied. The method of claim 3,
Wherein the driving means is a magnetic mixer capable of operating at 50 atmospheric pressure or less. The method of claim 3,
Wherein the gap between the fixed dispersion disk and the rotating disk spaced apart from the lower portion is in the range of 0.01 mm to 10 mm. The method of claim 3,
The number of revolutions of the rotating disk is a bubble column reactor applying a dynamic gas distributor, characterized in that proportional to the linear velocity of the syngas gas. The method of claim 3,
Wherein at least one of said rotary discs is installed in said compounding cylinder. The method of claim 10,
Wherein at least one of the inlet pipes is connected to a side of the blending cylinder below the portion where the rotating disk is installed. The method of claim 2,
Wherein the size of the aperture diameter of the fixed dispersion disk is in the range of 0.1 to 2 mm and the aperture ratio is in the range of 0.05 to 2.0%. The method of claim 1,
Wherein the catalyst contained in the slurry in the reactor body is selected from the group consisting of iron, cobalt, copper, potassium, cesium, sodium, molybdenum, tungsten, zinc, nickel, rubidium, rhodium and palladium having a particle size distribution of 0.1 - Or a mixture of two or more of them. The bubble column reactor is applied to a dynamic gas distributor. 14. The method according to any one of claims 1 to 13,
And a filtering means disposed in the upper portion of the reactor body for filtering the catalyst and flowing out only the synthetic fuel produced by the reaction to the outside of the reactor body,
Wherein an outflow pipe is connected to an upper end of the reactor body to discharge an unreacted synthesis gas and a chemical gas generated during the reaction to the outside of the reactor body. A dynamic gas distributor installed in communication with a reactor body of a bubble column reactor,
A mixing tube having an opening formed at an upper portion thereof to be connected to the reactor main body and temporarily storing the synthesis gas introduced through the inlet pipe and mixing the same at a constant composition and pressure;
Gas dispersing means for dispersing the synthesis gas introduced into the mixing vessel by rotation;
A fixed dispersion disk coupled to the open portion of the compounding vessel and having a plurality of openings formed in its surface to convert the bubble particles of the synthesized gas dispersed by the gas dispersion means into a uniform size;
And a second gas-liquid separator disposed in the second gas-liquid separator. 16. The fuel cell system according to claim 15,
A rotating disk spaced apart from a lower portion of the stationary dispersion disk to adjust an opening / closing cycle of the aperture;
Driving means disposed outside the compounding cylinder for rotating the rotary disk;
And a second gas-liquid separator disposed in the second gas-liquid separator. 17. The method of claim 16,
The rotating disk may be any one selected from a semicircular disk, a plurality of arc-shaped disks formed symmetrically, a semicircular disk having a plurality of openings, a plurality of arc-shaped disks formed with a plurality of openings, and a circular disk having a plurality of openings formed therein Wherein the gas distributor is a single gas-liquid separator. 17. The method of claim 16,
Wherein at least one of said rotary discs is provided in said compounding cylinder and at least one of said inlet pipes is connected to a side of said compounding cylinder below a portion where said rotary disc is installed. . 17. The method of claim 16,
Wherein the interval between the stationary dispersion disk and the rotating disk spaced apart from the bottom is in the range of 0.01 mm to 10 mm. 17. The method of claim 16,
Wherein the rotational speed of the rotating disk is proportional to the linear velocity of the syngas gas.

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